Conversion of lipids into olefins

ABSTRACT

A method of converting lipids to useful olefins includes reacting a mixture of lipids and a reactant olefin with microwave irradiation in the presence of ruthenium metathesis catalysts. The lipids may be unsaturated triacylglycerols or alkyl esters of fatty acids. The lipids may be sourced from renewable sources such as vegetable oil, waste cooking oil, or waste animal products.

CROSS-REFERENCE TO RELATED APPLICATION

The present application claims the priority benefit of U.S. Provisional Patent Application No. 62/213,879, filed on Sep. 3, 2015, the entire contents of which are incorporated herein by reference, for all purposes.

FIELD OF THE INVENTION

The present invention relates to methods of converting lipids into useful olefins.

BACKGROUND

More than 90% of the raw materials for today's chemical industry are petroleum feedstocks while only one-tenth of the feedstock comes from renewable resources. Considering the increasing importance of sustainability, there is interest on the development of fuels, chemicals and materials from renewable resources. The transformation of plant oils, due to their low cost, biodegradability and large scale availability, has received significant attention. In addition to large scale availability, a wide range of products can be obtained from plant oils which make them cost-effective and environment friendly alternative.

For chemical conversion and formation of new carbon-carbon double bonds, olefin metathesis is considered a versatile synthetic transformation tool and has been used in both pure and applied chemistry. Generally, olefin metathesis can be classified into ring-opening, ring closing and cross-metathesis. Metal-catalyzed olefin cross-metathesis (CM) has become a standard synthetic method with numerous industrial uses, including the well-known Shell Higher Olefin Process (SHOP). Olefin cross-metathesis is a catalytic reaction between two alkene molecules that results in redistribution of alkylidene groups. The cross-metathesis of an olefinic compound with ethylene is called ethenolysis, and a cross-metathesis with an olefin other than ethylene is called alkenolysis. Various efforts have been made on the conversion of plant oil derived fatty acids into products using ethylene metathesis (ethenolysis) chemistry. The production of olefins through ethenolysis may produce high value linear α-olefins which are direct antecedent to various applications including monomers for polymer synthesis, cosmetic ingredients, lubricants, detergents, soaps, perfumes, antimicrobial agents and renewable fuels.

Cross-metathesis of seed-oil derivatives and purified methyl oleate as a model substrate is known. However, these reactions are carried out in organic solvents and a high catalyst loading is required for effective conversion, which limits industrial scale viability of these processes, and particularly ethenolysis.

Purified methyl oleate has been used as a model substrate for metathesis. Relatively high turn over numbers (TONs) have been reported on the alkenolysis of methyl oleate using other olefins as ethylene surrogates in CM reactions. For example, the TON for CM of methyl oleate with propylene and 2-butene has achieved TONs as high as 192,900 and 470,000 respectively. However, metathesis with higher olefins results in the production of substantial amount of internal olefins, which are considered low value products compared to α-olefins produced through ethenolysis.

There remains a need in the art for methods of efficiently producing olefins from renewable fatty acid sources.

SUMMARY OF THE INVENTION

The present invention relates to the conversion of lipids such as plant oils and fatty acid methyl esters of plant oils, including canola oil, canola oil methyl esters or CMEs, recycled or waste cooking oil, and lipids extracted from animal sources, such as spent fowl, using ruthenium metathesis catalysts under microwave irradiation, to produce olefins. In one embodiment, the metathesis reactions are conducted under solvent-free microwave conditions and may provide relatively higher TON rates.

In one aspect, the invention may comprise a method of conversion of a lipid to an olefin product, comprising the steps of heating a mixture of unsaturated triacylglycerols or alkyl esters of unsaturated fatty acids and a reactant olefin with microwave irradiation, in the presence of a ruthenium complex catalyst. In some embodiments, the unsaturated triacylglycerols comprises a vegetable oil or a waste cooking oil, or wherein the alkyl esters of unsaturated fatty acids comprise methyl esters of fatty acids derived from a vegetable oil or waste cooking oil. The vegetable oil may comprise canola oil. The reactant olefin may comprise ethylene or 1,5-hexadiene. The ruthenium complex catalyst comprises one of Grubb's 1st generation or 2nd generation catalyst or Hoveyda-Grubb's 1st generation or 2nd generation catalyst, and may be present in a concentration between about 0.005 mole % and 0.5 mole %. The mixture may be heated to a temperature between about 30° C. and 80° C., preferably about 50° C. The reaction time may be between about 3 minutes to about 10 minutes, including ramping time and hold time.

In a preferred embodiment, the reactant mixture does not include a solvent.

In one embodiment, the unsaturated triacylglycerols may be derived from spent hen, extracted from spent hen using a solvent heated by microwave irradiation.

In preferred embodiments, very high effective TONs were achieved in ethenolysis and alkenolysis of canola oil methyl esters (CMEs) using ethylene and 1-5 hexadiene. In many cases the TONs higher than 500,000 were achieved. Surprisingly, in some cases the TONs as high as 1,561,583 and TOFs as high as 27,591 were achieved. Complete conversions were observed at 50° C. within few minutes.

BRIEF DESCRIPTION OF THE DRAWINGS

The drawings attached to or embedded in the description form part of the specification and are included to further demonstrate certain embodiments or various aspects of the invention. In some instances, embodiments of the invention can be best understood by referring to the accompanying drawings in combination with the detailed description presented herein. The description and accompanying drawings may highlight a certain specific example, or a certain aspect of the invention. However, one skilled in the art will understand that portions of the example or aspect may be used in combination with other examples or aspects of the invention.

FIG. 1A shows Grubbs (G) and Hoveyda-Grubbs (HG) first and second generation (1&2) catalysts. FIG. 1B shows a scheme showing products of ethenolysis (A); alkenolysis (B) of canola methyl esters (CME) waste cooking oil methyl esters (WOME) and direct ethenolysis of canola oil (C) under microwave conditions.

FIG. 2 shows GCMS spectrum of canola methyl esters (CME) and ethenolysis products.

FIG. 3 shows GCMS spectrum of waste cooking oil methyl esters (WOME) and its metathesis products with ethylene

FIG. 4 shows GCMS spectrum of canola methyl esters (CME) and alkenolysis products.

FIG. 5 shows GCMS spectrum of canola oil and its metathesis products with ethylene.

FIG. 6 shows a scheme showing possible products from ethenolysis of chicken FAME's (CF) under microwave conditions.

FIG. 7 shows GCMS spectrum of Chicken FAME's (CF) and its ethenolysis products.

DETAILED DESCRIPTION

The present invention relates to methods of converting unsaturated lipids into olefins. In one embodiment, the method comprises the metathesis of unsaturated triacylglycerols or alkyl esters of unsaturated fatty acids, with olefins such as ethylene and 1,5-hexadiene, with microwave irradiation and ruthenium complex catalysts, to produce alpha-olefins. Various embodiments encompass varying conditions, and different combinations of conditions, such as catalysts, their concentration, and time and temperature of reaction.

Use of microwave electromagnetic radiation for the cross metathesis reactions of vegetable oils with ethylene and 1,5-hexadiene may provide high conversion rate, TONs and turn over TOFs in a relatively short reaction time, preferably without any solvent at a relatively low concentration of ruthenium based catalysts. In some embodiments, more than 1.5 million TONs and up to 26,009 s⁻¹ turnover frequencies for ethenolysis of CME, around 618,000 TONs and 10,313 s⁻¹ TOFs for direct ethenolysis of canola oil and more than 1.6 million TONs and above 27,000 s⁻¹ TOFs for the cross metathesis of 1,5-hexadiene with CME may be achieved. Thus, the present methods may provide rapid and effective conversions of renewable oil and oil derivatives into useful chemicals.

The unsaturated fatty acids are preferably derived from a renewable source, such as unsaturated plant oils or from waste animal sources. In one embodiment, the unsaturated plant oil may comprise canola oil or a waste or used cooking oil. Triacylglycerols (TAGs) may be converted directly, or may first be transesterified to produce alkyl esters using known methods, such as with methanol, from which saturated esters may be substantially removed, for example via crystallization at lower temperature of −5° C. in the presence of acetone. When canola oil is transesterified with methanol, the resulting mixture of fatty acid esters (canola methyl esters or CME) comprises methyl oleate (67%), methyl linoleate (22%), and methyl linolenate (1%) with small quantities of some other saturated and unsaturated esters.

Olefin metathesis (OM) for the conversion of oleochemicals into valuable products has been facilitated by the well-defined, functional-group tolerant ruthenium alkylidene complexes developed by Grubbs et al.³¹ These catalysts can be handled in air and react selectively with olefins in the presence of various functional groups. However, the ratio of the rate of metathesis over the rate of catalyst decomposition determines the efficiency of an olefin metathesis catalyst. Reaction temperature and the use of solvents are known to impact catalyst efficiency and decomposition. Catalyst decomposition during extended reaction times and temperatures significantly affect TONs and product selectivity. However, the selectivity of ruthenium complexes for the production of α-olefins has been reported as poor.

In one embodiment, the method comprises a rapid conversion of canola oil and canola methyl esters (CME) and waste cooking oil methyl esters (WOME) into linear α-olefins under solvent-free, microwave-assisted ethenolysis and alkenolysis using ethylene and a diolefin (1,5-hexadiene). The reaction was investigated using varying reaction conditions, including temperature, time, catalysts screening and concentrations. For the calculation of effective TONs, two different approaches were used: 1) TONs calculated based on yield (TON_(Y)) as reported by Grubbs et al³¹ and 2) TONs calculated based on Me9DA (TON_(Me9DA)) as reported by Pederson et al.³⁵

For ethenolysis reactions of CME, a group of four different ruthenium based catalysts (Grubbs (G1 and G2) and Hoveyda-Grubbs (HG1 and HG2) shown in FIG. 1, was screened to assess their suitability under microwave irradiations at a temperature of about 50° C. for about 8 minutes (3 minutes ramping time+5 minutes hold time). The initial reactions were performed with catalyst loading of 0.1 mole % (moles of catalyst per mole of substrate). As can be seen from Table 1, the second generation catalysts (G2 & HG2) displayed better transformation of reactants into metathesis products compared to the first generation catalysts (G1 & HG1). The G2 catalyst was found more active under microwave conditions, and 0.5 mole % of G2 resulted in 98% conversions within about 2 to about 5 minutes. Under the same reaction conditions, G2 & HG2 displayed higher conversion rates (96%) with good selectivity, yield, TONs and TOFs (Table 1, entry 2 and 10) compared to G1 and HG1, which had conversion rates of 65% and 64% respectively (Table 1, entry 1 and 3). Considering higher conversion rates of second generation catalysts, G2 & HG2 were further investigated using lower catalyst loading (0.05 mole %) and shorter reaction time of 3.5 minutes (3 minutes of ramping time+thirty seconds hold time). Despite 50% decrease in catalyst loadings of G2 & HG2, from 0.1 mole % to 0.05 mole %, the conversion rates did not change significantly (95% and 96% respectively). However, a decrease in selectivity and yield for catalyst G2 was observed (Table 1, entry 4). Compared to G2, HG2 displayed higher selectivity (65%) and yield (84%), with improved TONy (157,371), TON_(Me9DA) (318,340) and TOFs (Table 1 and Table 1S entry 5).

Accordingly, HG2 may be a preferred catalyst under solvent free microwave conditions. HG2 catalyst was further studied at different temperatures (40, 50, 60 and 80° C.) and with lower catalyst loadings to optimize yield, selectivity, TONs and TOFs. An efficient conversion (96%) was still reached at all temperatures with 0.1 mole % of HG2 catalyst loading. However, lower selectivity, yield and TONs was observed at 40° C. (Table 1, entry 9). Ethenolysis at a temperature of 50° C. resulted in better selectivity (66%), yield (88%) and TONs (TONy 82,361, TON_(Me9DA) 165,090) compared to the reactions performed at 60° C. and 80° C. The increased temperature of 60° C. and 80° C. may have induced early decomposition of catalyst, which may account for reduced TONs (Table 1, entry 11 and 12). These investigations indicate that the solvent free microwave-assisted metathesis reactions may take place in a range of about 40 to about 80 degrees, and preferably at about 50° C.

Further ethenolysis reactions of CME were performed with lower concentration of HG2 catalyst. Further lowering the catalyst loading of HG2 from 0.05 to 0.01 mole % resulted in a significant increase in TONs (TONy 660,980, TON_(Me9DA) 1,561,583), TOFs (TOFy 11016 s⁻¹, TOF_(Me9DA) 26,009) with 70% yield and 60% selectivity for ethenolysis products over self-metathesis products (table 1 and 1 S entry 6). The TONy and TOFy values were further increased up to 1247129, and 20785 s⁻¹ respectively upon lowering the HG2 catalyst loading to 0.005 mole %, while slightly lowered when calculated on the basis of Me9DA only without affecting the conversion, selectivity and yield (table 1 and 1 S, entry 7). HG2 maintained higher conversion rate (95%) and exhibited the highest catalytic activity even at the lowest concentration of 0.005 mole %. Surprisingly, TONy (1,314,005) and TOFy (21,900 s⁻¹) values were obtained when further decreased concentration (0.002 mole %) of HG2 was used, while on the basis of Me9DA, decrease in TON_(Me9DA) (573,333) and TOF_(Me9DA) (9555) were observed as the selectivity of Me9DA lowered (table 1 and 1S, entry 8). Nevertheless, despite increase in TONy and TOFy, the decrease in loading of HG2 to 0.002 mole % significantly reduced conversion (69%), selectivity (42%) and yield (33%) suggesting that further decrease in catalyst loading will result in lower conversion, yield and selectivity. Values of 1,561,583 (TON_(Me9DA)) and TONy (1,314,005), which are almost 4.6 and 3.8 times higher respectively than the previous highest TONs achieved by ethenolysis of methyl oleate recently reported by Grubbs et al.³⁹ while 3.3 and 2.8 times higher respectively than the TONs obtained after butenolysis of methyl oleate described by Jackson et al.⁵⁹ using ruthenium systems. The possible terminal and internal olefins obtained after catalytic transformation of CME with ethylene are shown in the scheme shown in FIG. 1B, and were characterized by GCMS analysis (FIG. 2). For complete identification, the mixture was separated into 3 fractions; volatiles, hydrocarbons and esters,

TABLE 1 Ethenolysis of renewable canola methyl esters derived from canola oil Loading temp. time ^(a)conv. ^(b)selectivity ^(c)yield entry cat. (mole %) (° C.) (min.) (%) (%) (%) ^(d)TONy ^(e)TON_(Me9DA) 1 G1 0.1 50 5 65 74 49 46,027 126,578 2 G2 0.1 50 5 96 70 90 84,542 130,901 3 HG1 0.1 50 5 64 88 63 59,733 263,505 4 G2 0.05 50 0.5 95 32 57 107,208 82,510 5 HG2 0.05 50 0.5 96 65 84 157,371 318,340 6 HG2 0.01 50 1 96 60 70 660,980 1,561,583 7 HG2 0.005 50 1 95 52 66 1,247,129 1,165,693 8 HG2 0.002 50 1 69 42 33 1,314,005 573,333 9 HG2 0.1 40 3 96 46 62 58,492 136,290 10 HG2 0.1 50 1 96 66 88 82,361 165,090 11 HG2 0.1 60 1 96 64 85 80,265 150,109 12 HG2 0.1 80 1 96 69 89 83,771 171,781 ^(a)Conversions = 100 − [(final moles of reactants)100/(initial moles of reactants), ^(b)Selectivity = (moles of product 1 and 2)100/(total moles of products), ^(c)Yield = (moles of total products)100/(initial moles of reactants), ^(d)TONy = Yield (initial moles of reactants)/(moles of catalyst), ^(e)TON_(Me9DA) (turnover numbers based on Me9DA only) = 10,000 × (GC % of Me9DA)/(catalyst loading in mol ppm)

Although increased TONy from 82,361 to 1,314,005 without decrease in conversion rate were achieved by lowering the catalyst loading from 0.1 mole % to 0.002 mole % but yield and selectivity gradually decreased from 88% to 33% and 66% to 42% respectively as depicted in table 1. It has also been observed that decrease in reaction times under microwave irradiation resulted in higher conversion rate giving a record number of TOFs 26,009 s⁻¹ (table 1S, entry 6).

TABLE 1S Turnover frequency (TOF) of ethenolyzed canola methyl esters derived from canola oil entry ^(f)TOFy (S⁻¹) ^(g)TOF_(Me9DA) (S⁻¹) 1 153 421 2 281 436 3 199 878 4 3573 2750 5 5245 10,611 6 11,016 26,009 7 20,785 19,428 8 21,900 9555 9 325 757 10 1372 2751 11 1337 2501 12 1396 2863 ^(f)TOFy = TONy/time (sec.). Calculated from TON's obtained using total yield of products ^(g)TOF_(Me9DA) = TON_(Me9DA)/time (sec.). Caluclated from TON'S obtained by GC % of Me9DA only

Ethenolysis of waste cooking oil methyl esters (WOME) was carried out under conditions found to be optimal for ethenolysis of CME, but with different catalyst loadings of HG2 (table 2). A highest conversion rate of 96% was observed with all catalyst loadings (0.1 mole % to 0.005 mole %) in one minute of reaction time. With 0.1 mole % of catalyst loading, 63% selectivity and 75% yield was obtained, providing 56117 TONy and 935 s⁻¹ TOFs. Decreasing the catalyst contents to 0.005 mole % resulted in a drop of selectivity to 59% and yield to 72%, while enhanced values of TONs (TONy 1,073,466, TON_(Me9DA) 1,078,102) and TOFs (TOFy 17,891 s⁻¹, TOF_(Me9DA) 17,968) were obtained (table 2 and 2S, entry 3). Again TONs obtained in this case are more than three times higher than the previous highest TONs 340000 achieved by ethenolysis of methyl oleate reported by Grubbs et al⁶⁰. The product components obtained after ethenolysis of WOME were characterized by GC analysis (FIG. 3) and found to be similar to those described for the ethenolysis of CME (FIG. 2).

TABLE 2 Ethenolysis of methyl fatty esters (WOME) derived form waste coocking oil Loading temp. time ^(a)conv. ^(b)selectivity ^(c)yield entry cat. (mole %) (° C.) (min.) (%) (%) (%) ^(d)TONy ^(e)TON_(Me9DA) 1 HG2 0.1 50 1 96 63 75 56,117 107,574 2 HG2 0.05 50 1 96 57 70 104,551 205,247 3 HG2 0.005 50 1 96 59 72 107,3466 1,078,102 ^(a)Conversions = 100 − [(final moles of reactants)100/(initial moles of reactants), ^(b)Selectivity = (moles of product 1 and 2)100/(total moles of products), ^(c)Yield = (moles of total products)100/(initial moles of reactants), ^(d)TONy = Yield (initial moles of reactants)/(moles of catalyst), ^(e)TON_(Me9DA) (turnover numbers based on Me9DA only) = 10,000 × (GC % of Me9DA)/(catalyst loading in mol ppm)

TABLE 2S Tunrover frequency (TOF) of ethenolyzed WOME entry ^(f)TOFy (S⁻¹) ^(g)TOF_(Me9DA) (S⁻¹) 1 935 1792 2 3485 3420 3 17,891 17968 ^(f)TOFy = TONy/time (sec.). Calculated from TON's obtained using total yield of products ^(g)TOF_(Me9DA) = TON_(Me9DA)/time (sec.). Caluclated from TON's obtained by GC % of Me9DA only

Despite higher TONs than ethenolysis, alkenolysis with higher olefins typically results in substantial amounts of undesired internal olefins. The cross-metathesis with diolefin such as 1,5-hexadiene should results in terminal metathesis products due to the presence of both terminal double bonds (FIG. 4). Therefore, alkenolysis of canola methyl esters with 1,5-hexadiene was also performed using microwave radiations. Similar to ethenolysis, G1, G2, HG1 and HG2 were screened with 0.1 mole % catalyst loadings at 50° C. temperature. No reaction products were observed with 0.1 mole % of first generation catalysts (G1 & HG1) for 8 minutes reaction time under microwave conditions. Surprisingly, G2 & HG2 gave the highest conversion rate of 99% within about 8 minutes (˜3 minutes of ramping time+5 minutes hold time) with effective TONy of 90,728 and 86,639 respectively calculated on basis of yield, and TON_(Me9DA) 84,120 and 133,890 respectively measured on the basis of Me9DA only (table 4, entry 2 and 4). While 81% selectivity and 96% yield was achieved with G2, which is slightly higher compared to 73% selectivity and 92% yield obtained by HG2 catalyst (table 3). Both of these catalysts further studied at lower catalyst loading of 0.05 mole % for a reaction time of ˜3.5 min (˜3 min ramping time+30 seconds hold time). A sharp decrease in conversion rate, yield and TONs were observed with catalyst G2, the conversions decreased to 27%, yield declined from 96% to 23%, and TONy reduced from 90728 to 44184, with modest selectivity of 73% (table 3, entry 5). While in case of HG2, improved selectivity (82%), yield (99%), TONs as well as TOFs were observed with similar conversion rate (table 3 and 3S, entry 6. These results suggest that HG2 is a preferred catalyst for alkenolysis of fatty acid esters under microwave conditions.

Decreasing the catalyst loading to 0.01 mole % still provided high conversions with slight decrease in selectivity and yield, with a significant increase in TONy (791,277), TON_(Me9DA) (1,655,474) and TOFy (13188 s⁻¹), TOF_(Me9DA) 27,591 values (table 3 and 3S, entry 7). These TONs are about 1.7-3.5 times higher than the previous highest TONs (470000) reported for the butenolysis of methyl oleate by Jackson et al. Further lowering of catalyst contents below 0.01 mole % resulted in a very low conversions for alkenolysis reactions.

TABLE 3 Cross metathesis of renewable FAME's derived from canola oil (CME) with 1,5-hexadiene Loading temp. time ^(a)conv. ^(b)selectivity ^(c)yield entry cat. (mole %) (° C.) (min.) (%) (%) (%) ^(d)TONy ^(e)TON_(Me9DA) 1 G1 0.1 50 5 0 0 0 0 0 2 G2 0.1 50 5 99 81 96 90,728 84,120 3 HG1 0.1 50 5 0 0 0 0 0 4 HG2 0.1 50 5 99 73 92 86,639 133,890 5 G2 0.05 50 0.5 27 73 23 44,184 104,184 6 HG2 0.05 50 0.5 99 82 99 186,025 234,787 7 HG2 0.01 50 1 98 70 84 791,277 1,655,474 8 HG2 0.1 45 5 82 67 82 68,260 189,163 9 HG2 0.1 60 1 99 72 96 90,531 83,636 10 HG2 0.1 80 1 93 73 73 76,948 196,436 ^(a)Conversions = 100 − [(final moles of reactants)100/(initial moles of reactants), ^(b)Selectivity = (moles of product 1 and 2)100/(total moles of products), ^(c)Yield = (moles of total products)100/(initial moles of reactants), ^(d)TONy = Yield (initial moles of reactants)/(moles of catalyst), ^(e)TON_(Me9DA) (turnover numbers based on Me9DA only) = 10,000 × (GC % of Me9DA)/(catalyst loading in mol ppm)

TABLE 3S Turnover frequency (TOF) of Cross metathesis of FAME'S derived from canola oil (CME) with 1,5-hexadiene entry ^(f)TOFy (S⁻¹) ^(g)TOF_(Me9DA) (S⁻¹) 1 0 0 2 302 280 3 0 0 4 288 446 5 1472 3472 6 6200 7826 7 13,188 27,591 8 227 630 9 1508 1393 10 1282 3273 ^(f)TOFy = TONy/time (sec.). Calculated from TON'S obtained using total yield of products ^(g)TOF_(Me9DA) = TON_(Me9DA)/time (sec.). Caluclated from TON'S obtained by GC % of Me9DA only

Generally speaking, olefin metathesis is an equilibrium process. Although kinetic products can be isolated under certain specific conditions, generally alkylidene complexes can be identified when there are higher concentrations of olefins in the mixture. Therefore, the olefins used for the cross-metathesis reactions of the present invention may comprise the formula shown below, where R=H, ethyl, pentyl, octyl, 2-propenyl, 3-butenyl, undec-2-enyl, dodec-3-enyl, and oct-2,5-dienyl. Potential alkylidene complexes with the catalysts are shown below:

Direct ethenolysis of canola oil was also studied under similar conditions mentioned for ethenolysis of CME. More than 94% conversions were obtained in one minute of reaction time (table 4) with two different loadings of HG2 catalyst (0.05 mole %, and 0.01 mole %). Anomalous behavior can be seen in table 4, as 4% selectivity and 34% yield was obtained with 0.05 mole % catalyst loading, while an increased selectivity (19%) and yield (49%) was achieved, when catalyst loading was lowered to 0.01 mole %. In spite of higher conversion rate, lower selectivity and yield was obtained, as most of the reactant component cis-oleate (C18:1 C, FIG. 5) has transformed into trans-oleate (C18:1 t) during the reaction. This could be the result of uncontrolled and/or lower ethylene pressure, as it was maintained manually. A notable increase in TONy from 67,940 to 495,200, TON_(Me9DA) form 48,484 to 618,790 and TOFy from 1132 s⁻¹ to 8253 s⁻¹, TOF_(Me9DA) from 808 to 10,313 s⁻¹ were observed, when catalyst contents were decreased from 0.05 mole % to 0.01 mole %. The mixture of metathesis products obtained (Scheme 2) was transesterified before characterization with GCMS (FIG. 5).

TABLE 4 Ethenolysis of canola oil (TAG's) Loading temp. time ^(a)conv. ^(b)selectivity ^(c)yield entry cat. (mole %) (° C.) (min.) (%) (%) (%) ^(d)TONy ^(e)TON_(Me9DA) 1 HG2 0.05 50 1 95 4 34 67,940 48,484 2 HG2 0.01 50 1 94 19 49 495,200 618,790 ^(a)Conversions = 100 − [(final moles of reactants)100/(initial moles of reactants), ^(b)Selectivity = (moles of product 1 and 2)100/(total moles of products), ^(c)Yield = (moles of total products)100/(initial moles of reactants), ^(d)TONy = Yield (initial moles of reactants)/(moles of catalyst), ^(e)TON_(Me9DA) (turnover numbers based on Me9DA only) = 10,000 × (GC % of Me9DA)/(catalyst loading in mol ppm)

TABLE 4S Tunrover frequency (TOF) of ethenolyzed canola oil (TAG's) entry ^(f)TOFy (S⁻¹) ^(g)TOF_(Me9DA) (S⁻¹) 1 1132 808 2 8253 10,313 ^(f)TOFy = TONy/time (sec.). Calculated from TON'S obtained using total yield of products ^(g)TOF_(Me9DA) = TON_(Me9DA)/time (sec.). Caluclated from TON'S obtained by GC % of Me9DA only

Ethenolysis of methyl oleate has been extensively studied in the prior art. To compare the ethenolysis results of renewable fatty acid esters, ethenolysis of methyl oleate was performed in the same manner as described herein for canola methyl esters, Cross metathesis of methyl oleate with ethylene results in the formation of two cross 1 (methyl 9-decenoate) and 2 (1-decene) and two self 6 (dimethyl 9-octadecene-1,18-dioate) and 7 (9-octadecene) metathesis products as these products are shown in FIG. 2. Ethenolysis of methyl oleate was conducted using HG2 catalyst with two different concentration of 0.005 and 0.01 mole % providing almost 94% conversion in all cases (table 5). A good yield (72%), selectivity (65%) and TON_(Me9DA) (1,222,875) were obtained with 0.01 mole % loading of catalyst (table 5, entry 3). whereas decreasing catalyst loading to 0.005 mole %, a substantial decrease in yield (40%), selectivity (36%) and TON_(Me9DA) (794,285) were observed (table 5, entry 2). The TON's calculated on the basis of yield was found to be highest (806,000) with 0.005 mole % loading of catalyst (table 5, entry 2).

Without restriction to a theory, the lower yield and selectivity even with higher conversion rate in case of 0.005 mole % loading of catalyst are likely due to formation of trans methyl oleate during the reaction. A good number of TOF's values were also observed in ethenolysis of methyl oleate (table 5S) providing the highest TOF_(Me9DA) value of 20,380 with catalyst loading of 0.01 mole % (table 5S, entry 3).

The results given in table 5 shows that ethenolysis of methyl oleate displayed slightly lower yield, selectivity and TON's when compared with ethenolysis of CME. With catalyst loading of 0.01 mole %, the observed ethenolysis TON_(Me9DA) (1.2 million) for methyl oleate (table 5, entry 3) were found to be 20% less than the TON_(Me9DA) (1.5 million) obtained after ethenolysis of CME (table 1, entry 6). Lowering the catalyst loading to 0.005 mole % in the reaction of methyl oleate ethenolysis, resulted in a significant decrease in TON_(Me9DA) to 0.79 million (table 5, entry 2), while ethenolysis of CME still displayed an efficient value of TON_(Me9DA) 1.16 million (table 1, entry 7). The less yield, selectivity and TON's in case of methyl oleate ethenolysis can be attributed to less purity of methyl oleate (99%) as it effects the efficiency of reaction⁵⁹. Despite that, these TONy 806,000 (table 5, entry 2), TON_(Me9DA) 1,222,857 (table 5, entry 3), and TOFs (TOFy 13433 s⁻¹, TOF_(Me9DA) 20,380 in table 5S) for the ethenolysis of methyl oleate are the highest values.

TABLE 5 Ethenolysis of methyl oleate Loading temp. time ^(a)conv. ^(b)selectivity ^(c)yield entry cat. (mole %) (° C.) (min.) (%) (%) (%) ^(d)TONy ^(e)TON_(Me9DA) 1 HG2 0.005 50 1 94 19 34 688,000 372,380 2 HG2 0.005 50 1 94 36 40 806,000 794,285 3 HG2 0.01 50 1 94 65 72 721,000 1,222,857 4 HG2 0.01 50 1 92 56 75 750,500 972,380 ^(a)Conversions = 100 − [(final moles of reactants)100/(initial moles of reactants), ^(b)Selectivity = (moles of product 1 and 2)100/(total moles of products), ^(c)Yield = (moles of total products)100/(initial moles of reactants), ^(d)TONy = Yield (initial moles of reactants)/(moles of catalyst), ^(e)TON_(Me9DA) (turnover numbers based on Me9DA only) = 10,000 × (GC % of Me9DA)/(catalyst loading in mol ppm)

TABLE 5S Tunrover frequency (TOF) of ethenolyzed methyl oleate entry ^(f)TOFy (S⁻¹) ^(g)TOF_(Me9DA) (S⁻¹) 1 11,466 6206 2 13,433 13,238 3 12,016 20,380 4 12,508 16,206 ^(f)TOFy = TONy/time (sec.). Calculated from TON's obtained using total yield of products ^(g)TOF_(Me9DA) ⁼ TON_(Me9DA)/time (sec.). Caluclated from TON's obtained by GC % of Me9DA only

In an alternative embodiment, the lipids may be sourced from a renewable or waste animal byproduct. For example, spent hens are a poultry industry byproduct and may be used as a potential source of lipids. In the poultry industry, manufacturers have few ways and means of disposing spent flocks, not all of which are economically feasible. A whole spent hen has ˜1.8 kg meat and on average the whole spent hen contains about 15% fat, which represents a significant resource of lipids which could be utilized. Lipids may be extracted from ground spent fowl using microwave extraction, for example.

Therefore, microwave assisted ethenolysis of fatty acid methyl esters (FAMEs) derived from spent fowl was conducted using G2 and HG2. The possible products after ethenolysis of spent fowl FAME's are shown in the scheme shown in FIG. 6, while the products obtained and identified by GCMS are shown in FIG. 7. In one embodiment, the reactions were performed using G2 and HG2 catalysts with loadings of 0.01 mole %. Among these two catalysts, HG2 displayed better conversion rate (92%) as compared to G2, which showed only 64% conversion. GCMS spectrum of FAME's after treatment with HG2 catalyst (FIG. 7) also shows maximum conversion of starting materials (methyl oleate, C18:1 and methyl linoleate, C18:2) into metathesis products. Over all, HG2 catalyst was found to be effective providing 44% selectivity, 57% yield, 568,800 TONy, 891,982 TON_(Me9DA) and 9,480 S⁻¹ TOFy, 14,866 S⁻¹ TOF_(Me9DA) (table 5 & 5S, entry 2), while G2 catalyst gave 47% selectivity, 36% yield, 365,200 TONy, 864,462 TON_(Me9DA) and 6,086 S⁻¹ TOFy, 14,407 S⁻¹ TOF_(Me9DA) (table 5 & 5S, entry 1). Depending on these results, HG2 catalyst was further used with lower loading of 0.005 mole %. A good conversion rate (82%), selectivity (45%) and yield (50%) were obtained representing highest value of effective TON's (1,010,800 TONy, 929,844 TON_(Me9DA)) and TOF's (16846 S⁻¹ TOFy, 15,497 S⁻¹ TOF_(Me9DA)) given in table 5 & 5S, entry 3. So the value of about one million TON's, and around 16000 S⁻¹ TOF's are the highest values achieved for the first time for ethenolysis of FAME's derived from spent fowl.

TABLE 6 Ethenolysis of FAME's derived from spent foul Loading temp. time ^(a)conv. ^(b)selectivity ^(c)yield entry cat. (mole %) (° C.) (min.) (%) (%) (%) ^(d)TONy ^(e)TON_(Me9DA) 1 G2 0.01 50 1 64 47 36 365,200 864,462 2 HG2 0.01 50 1 92 44 57 568,800 891,982 3 HG2 0.005 50 1 82 45 50 1,010,800 929,844 ^(a)Conversions = 100 − [(final moles of reactants)100/(initial moles of reactants), ^(b)Selectivity = (moles of product 1 and 2)100/(total moles of products), ^(c)Yield = (moles of total products)100/(initial moles of reactants), ^(d)TONy = Yield (initial moles of reactants)/(moles of catalyst), ^(e)TON_(Me9DA) (turnover numbers based on Me9DA only) = 10,000 × (GC % of Me9DA)/(catalyst loading in mol ppm)

TABLE 6S Tunrover frequency (TOF) of ethenolyzed chicken FAME's entry ^(f)TOFy (S⁻¹) ^(g)TOF_(Me9DA) (S⁻¹) 1 6,086 14,407 2 9,480 14,866 3 16,846 15,497 ^(f)TOFy = TONy/time (sec.). Calculated from TON'S obtained using total yield of products ^(g)TOF_(Me9DA) = TON_(Me9DA)/time (sec.). Caluclated from TON's obtained by GC % of Me9DA only

Examples

All reactions described herein were performed on a CEM-Discover (120 V, Matthews, USA), a source of microwave irradiation in 10 mL sealed tube, while infrared mode was used to measure the temperature of the reaction contents. To identify the components, GC-MS analyses of all samples were conducted on Agilent 6890N (USA) gas chromatograph, fitted with a fused silica capillary column SP2560 (100 m×0.25 mm×0.2 μm film thickness) and detector 5975B inert XL MSD. The sample volume of 2 μL was injected, while the injector temperature was set to 240° C. and a split mode with ratio of 20:1 was used. The initial temperature of oven was set to 45° C. and held for 4 minutes. The temperature was then increased to 175° C. with a ramp rate of 13° C. min⁻¹; hold for 27 minutes, and further ramped at 4° C. min⁻¹ to 215° C. and hold for 35 minutes. The mass scanning range of 30-1000 amu at 1.55 scan per second was performed. Helium gas was used as a mobile phase with a constant flow rate of 1.3 mL/min.

The hydrocarbon fractions were characterized on Agilent 7980A (USA) instrument using HP5 column (30 m×0.32 mm×0.25 μm film thickness), coupled with inert EI MSD with triple axis detector (5975C, Agilent, USA). The injection volume of 1 μL was used with injector temperature of 250° C. in a splitless mode. The oven initial temperature of 50° C. was set and held for two minutes. The temperature was increased at a ramp rate of 5° C. min⁻¹ to 325° C. and then held for five minutes. The MS scanning range of 50-600 amu was applied with a scan rate of 2.66 per second. A constant flow rate of 4.4 mL/min of helium gas was used as mobile phase.

While Perkin Elmer GC-FID Clarus 500 instrument (USA) equipped with flame ionization detector was used for quantitative analysis to measure the conversion rate, selectivity and yield of all samples. The temperature was set at 280° C. for detector, while 240° C. for injector. The air and hydrogen gases were used as a carrier with the flow rate of 450 and 45 mL/min respectively. While the column used and rest of the conditions were same as mentioned above for GC-MS instrument Agilent 6890N.

¹H NMR spectra of selected samples were recorded after dissolving in deuterated chloroform at 400 MHz frequency on a Varian INOVA instrument at a temperature of 27° C.

Canola oil, methyl oleate (97%), Grubb's catalyst 1^(st) generation (G1, 97%), Grubb's catalyst 2^(nd) generation (G2), Hoveyda-Grubb's catalyst 1^(st) generation (HG1), Hoveyda-Grubb's catalyst 2^(nd) generation (HG2, 97%), 1,5-hexadiene (97%), ethyl vinyl ether (≧98%), potassium hydroxide (≧85%), sodium chloride (≧99.5%), anhydrous sodium sulphate (≧99%), dichloromethane (≧99.5%), methanol (≧99.8%) and acetone (≧99.9%) were obtained from sigma Aldrich. While ethylene gas (Mathesons, polymer grade, CAS: 74-85-1), silica gel used for column chromatography (70-230 mesh, 60 Å), flash silica (Silicycle, 40-63 μm, 230-400 mesh), thin layer aluminium chromatographic plates (Macherey-Nagel, 0.20 mm thick, 20×20 cm size, UV254), ethyl acetate (fisher, 99.9%), n-hexane (Caledon) were purchased and used as such.

Methanolic Transesterification of Canola Oil and Waste Cooking Oil.

Methanolic transesterification of canola oil and waste cooking oil into their fatty esters was performed using KOH as a base according to the published method of Arshad, M. et al.⁶⁵

Separation of Saturated Esters by Crystallization Method.

For best results in metathesis reactions, saturated esters were removed from transesterified canola methyl esters (CME) and waste cooking oil methyl esters (WOME) by a crystallization method. Separation by column chromatography is difficult due to their almost same R_(f) value. For their separation, these esters were dissolved in acetone and kept overnight at a temperature of −5° C. The volume of acetone used was equal to the volume of esters. Saturated esters solidify at this lower temperature and were separated by filtration at similar temperature. This process was repeated three times to remove maximum amount of saturated esters. The obtained esters which were mostly unsaturated were dried and passed through a column of flash silica before proceeding for metathesis reactions.

General Procedure for Ethenolysis of Methyl Fatty Esters.

Specific amount methyl fatty esters were charged in a 10 mL glass vial having Teflon™ coated stirring bar and was purged with nitrogen gas for five minutes. An appropriate amount of catalyst (table 1) was weighed in a glove box under an atmosphere of nitrogen and was added into the reaction vial. The reaction vial was sealed and brought to the ethylene line. The reaction vessel was purged with ethylene gas for five minutes and then ethylene was liquefied into the reaction vial to a volume of about 0.05 mL by cooling the vial in liquid nitrogen. The reactions were conducted in sealed reaction vessels at specified temperatures. Microwave power was varied by the instrument in order to reach and maintain the set temperature. The reactions were run in duplicate and in some cases in triplicate runs were carried out. The pressure variation during ethenolysis was between 80 and 120 PSI with an average pressure for each reaction was ˜100 PSI. The set maximum power for the instrument was 250 W. The reaction was run for specific time interval at a suitable temperature to get maximum conversions of reactants into product components. The ramp time to attain the required temperature was typically about 3 minutes. After reaction completion, ethyl vinyl ether (0.5 mL) was added into the reaction mixture to deactivate the catalyst and was passed through a plug of flash silica to remove the catalyst. The product components were characterized by GCMS and quantified with GC-FID by considering naturally occurring methyl palmitate (C16:0) in the canola oil and/or methyl heptadecanoate (C17:0) as an internal standard.

Ethenolysis of Canola Oil.

Canola oil was first passed through a column of flash silica and anhydrous magnesium sulphate to remove colored pigments and moisture contents. Afterwards, it was proceeded for cross metathesis reactions with ethylene in the presence of catalyst HG2 using identical conditions and/or methodology as mentioned for ethenolysis of CME.

Separation of Components

A volatile fraction was collected right after the completion of ethenolysis reaction containing 1,4-petadiene (4) and 1-butene (5) and was characterized by GCMS (Figure X supplementary information). The remaining mixture of ethenolyzed components were separated into three major fractions; hydrocarbons, methyl esters and pure dimethyl octadec-9-enedioate (6) with the help of silica gel column chromatography using an eluent system of 1-5% ethyl acetate in hexane. These fractions were further characterized by GCMS (supporting info). The hydrocarbon and methyl esters fractions were subjected to distillation separately to purify some of the major components. ¹H NMR of those purified components is provided in the supporting info.

Cross Metathesis of Canola Methyl Esters with 1,5-Hexadiene.

In a glove box under an inert atmosphere of nitrogen, an appropriate amount of catalyst (table. 4) was weighed and added into the reaction vile containing purified canola methyl esters (1 Eq.) degassed with inert nitrogen and equipped with a stirring bar. The reaction vessel was sealed and purged with nitrogen gas for five minutes followed by the addition of 1,5-hexadiene (2 Eq.) with the help of glass syringe. The sealed reaction vessel was placed in a microwave reactor having similar reaction conditions as have been mentioned for ethenolysis of CME. After reaction completion, ethyl vinyl ether (0.5 mL) was added into the reaction mixture to deactivate the catalyst and was passed through a plug of flash silica to remove the catalyst contents. The product components were characterized by GCMS and quantified with GC-FID by considering naturally occurring methyl palmitate (C16:0) in the canola oil and methyl heptadecanoate (C17:0) as an internal standard.

Extraction of Lipids from Chicken Using 80 mL Microwave Vessel Assembly

The following conditions were used for the extraction of lipids using microwave from the fresh ground chicken.

Temper- Hold Pres- Recovery ature Time sure Power of lipids (° C.) (minutes) (Psi) (W) Stirring MaxPower (%) 80 10 250 250 High On 99.77

Around 15 g of ground chicken was treated with the microwave, twice. The first treatment was in 25 mL of hexane as solvent and the second with 25 mL of chloroform. The extracts were then combined and filtered using filter paper. Sodium sulfate was used to remove the moisture from the extract. The solvents were then evaporated with a rotary evaporator. Several repetitions were made to extract the crude lipids in large quantity.

Methanolic Transesterification of Triacylglycerides from Spent Fowl.

Methanolic transesterification of triacylglycerides extracted from spent fowl was performed using KOH as a base according to the published method of Arshad, M. et al.⁶⁵

The transesterified fatty acid methyl esters (FAME's) were purified by silica gel column chromatography using an eluent mixture of 1% ethyl acetate in hexane. The pure FAME's were passed through a column of flash silica and anhydrous sodium sulphate prior to use.

General Procedure for Ethenolysis of FAME's from Spent Fowl.

A Specific amount FAME's derived from spent fowl were charged in a 10 mL glass vial having Teflon™ coated stirring bar and was purged with nitrogen gas for five minutes. An appropriate amount of catalyst (table 5) was weighed in a glove box under nitrogen atmosphere and was added into the reaction vial. The reaction vial was sealed and brought to the ethylene line. The reaction vessel was purged with ethylene gas for five minutes and then ethylene was liquefied into the reaction vial to a volume of about 0.5 mL by cooling the vial in liquid nitrogen. The reactions were conducted in sealed reaction vessels at specified temperatures. The power is usually adopted by the instrument to reach and maintain the set temperature. The reactions in duplicate runs were carried out. The pressure variation during ethenolysis was between 100 and 150 PSI with an average pressure for each reaction was 120 PSI. The set maximum power for the instrument was 250 W. The reaction was run for specific time interval at a suitable temperature to get maximum conversions of reactants into product components. The ramp time to attain the required temperature was ˜3 minutes. After reaction completion, the reaction mixture was passed through a plug of flash silica to remove the catalyst. The product components were characterized by GCMS and quantified with GC-FID by considering naturally occurring methyl palmitate (C16:0) in the fats of spent foul and/or methyl heptadecanoate (C17:0) as an internal standard.

DEFINITIONS AND INTERPRETATION

All terms and phrases used in this specification have their ordinary meanings, as one of skill in the art would understand, except where specifically defined. Such ordinary meanings may be obtained by reference to technical dictionaries, such as Hawley's Condensed Chemical Dictionary 14^(th) Edition, by R. J. Lewis, John Wiley & Sons, New York, N.Y., 2001.

To the extent that the following description is of a specific embodiment or a particular use of the invention, it is intended to be illustrative only, and not limiting of the claimed invention. The following description is intended to cover all alternatives, modifications and equivalents that are included in the spirit and scope of the invention, as defined in the appended claims. References in the specification to “one embodiment”, “an embodiment”, etc., indicate that the embodiment described may include a particular aspect, feature, structure, or characteristic, but not every embodiment necessarily includes that aspect, feature, structure, or characteristic. Moreover, such phrases may, but do not necessarily, refer to the same embodiment referred to in other portions of the specification. Further, when a particular aspect, feature, structure, or characteristic is described in connection with an embodiment, it is within the knowledge of one skilled in the art to affect or connect such aspect, feature, structure, or characteristic with other embodiments, whether or not explicitly described.

The corresponding structures, materials, acts, and equivalents of all means or steps plus function elements in the claims appended to this specification are intended to include any structure, material, or act for performing the function in combination with other claimed elements as specifically claimed.

It is further noted that the claims may be drafted to exclude any optional element. As such, this statement is intended to serve as antecedent basis for the use of exclusive terminology, such as “solely,” “only,” and the like, in connection with the recitation of claim elements or use of a “negative” limitation. The terms “preferably,” “preferred,” “prefer,” “optionally,” “may,” and similar terms are used to indicate that an item, condition or step being referred to is an optional (not required) feature of the invention.

The singular forms “a,” “an,” and “the” include the plural reference unless the context clearly dictates otherwise. The term “and/or” means any one of the items, any combination of the items, or all of the items with which this term is associated.

As will be understood by one skilled in the art, for any and all purposes, particularly in terms of providing a written description, all ranges recited herein also encompass any and all possible sub-ranges and combinations of sub-ranges thereof, as well as the individual values making up the range, particularly integer values. A recited range (e.g., weight percents or carbon groups) includes each specific value, integer, decimal, or identity within the range. Any listed range can be easily recognized as sufficiently describing and enabling the same range being broken down into at least equal halves, thirds, quarters, fifths, or tenths. As a non-limiting example, each range discussed herein can be readily broken down into a lower third, middle third and upper third, etc. As will also be understood by one skilled in the art, all language such as “up to”, “at least”, “greater than”, “less than”, “more than”, “or more”, and the like, include the number recited and such terms refer to ranges that can be subsequently broken down into sub-ranges as discussed above. In the same manner, all ratios recited herein also include all sub-ratios falling within the broader ratio.

The term “about” can refer to a variation of +5%, +10%, +20%, or +25% of the value specified. For example, “about 50” percent can in some embodiments carry a variation from 45 to 55 percent. For integer ranges, the term “about” can include one or two integers greater than and/or less than a recited integer at each end of the range. Unless indicated otherwise herein, the term “about” is intended to include values and ranges proximate to the recited range that are equivalent in terms of the functionality of the composition, or the embodiment.

REFERENCES

The following references are incorporated by reference herein for all purposes, where permitted, as though reproduced herein in their entirety.

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What is claimed is:
 1. A method of conversion of a lipid to an olefin product, comprising the steps of heating a mixture of unsaturated triacylglycerols or alkyl esters of unsaturated fatty acids and a reactant olefin with microwave irradiation, in the presence of a ruthenium complex catalyst.
 2. The method of claim 1 wherein the unsaturated triacylglycerols comprises a vegetable oil, waste cooking oil, or wherein the alkyl esters of unsaturated fatty acids comprise methyl esters of fatty acids derived from a vegetable oil or waste cooking oil.
 3. The method of claim 1 wherein the reactant olefin comprise ethylene or 1,5-hexadiene.
 4. The method of claim 1 wherein the ruthenium complex catalyst comprises one of Grubb's 1st generation or 2nd generation catalyst or Hoveyda-Grubb's 1st generation or 2nd generation catalyst.
 5. The method of claim 1 wherein the mixture is heated to a temperature between about 30° C. and 80° C.
 6. The method of claim 5 wherein the reaction temperature is 50° C.
 7. The method of claim 1 wherein the mixture does not include a solvent.
 8. The method of claim 4 wherein the catalyst is present in a concentration between about 0.005 mole % and 0.5 mole %.
 9. The method of claim 8 wherein the catalyst is HG2.
 10. The method of claim 5 wherein the reaction time is between about 3 minutes to about 10 minutes, including ramping time and hold time.
 11. The method of claim 1 wherein the unsaturated triacylglycerols are derived from spent hen.
 12. The method of claim 11 wherein the unsaturated triacylglycerols are extracted from spent hen using a solvent heated by microwave irradiation. 